Apparatus for direct reduction of iron using high sulfur gas

ABSTRACT

A method and apparatus for the direct reduction of iron oxide utilizing sulfur-containing gas such as coke oven gas for the process gas. Sulfur-containing gas is heated and injected above the reduction zone to transfer the sulfur to the hot burden. The apparatus includes an upper bustle zone for prereduction and sulfur transfer and a lower bustle zone for the final reduction of the burden to metallized iron.

BACKGROUND OF THE INVENTION

The direct reduction of iron oxide, in such forms as agglomeratedpellets or lump ore, to metallic iron in the solid state has in recentyears become a commercial reality in many direct reduction plantsthroughout the world. The combined annual capacity of these plantscurrently in operation or under construction is in excess of 15 millionmetric tons of direct reduced iron product, which is used primarily asfeedstock for electric arc steelmaking furnaces. The world demand foradditional direct reduced iron is projected to increase at a substantialrate for many years to satisfy a growing world need for such feedstock,as additional electric arc furnace steelmaking plants are constructed.

The majority of the commercial plants producing direct reduced ironutilize natural gas as the source of reductant. The natural gas isreformed to produce the reductants CO and H₂. The most energy efficientand most productive of the commercial natural gas based direct reductionplants are the Midrex plants which include continuous catalyticreforming of natural gas using as reforming oxidants the CO₂ andresidual water vapor in cooled, recycled, spent reducing gas from thereduction furnace, as taught in U.S. Pat. No. 3,748,120.

In the catalytic reforming of natural gas or otherhydrocarbon-containing gases, it is essential to maintain a very lowlevel of sulfur in the gas mixture being reformed, as is well recognizedin the art of catalytic reforming, in order to avoid sulfur poisoning ofthe catalyst. The maximum sulfur level which can be tolerated in thereforming, in order to avoid catalyst poisoning, is approximately 2 to 3parts per million by volume (ppmv) in the mixture being reformed. Toachieve this very low level of sulfur often requires complicated andexpensive desulfurization of the gas before it can be utilized asprocess fuel.

Coke oven gas is available as a fuel in many of the industrial countriesof the world. However, coke over gas includes certain sulfur containingcomponents such as COS and thiophene.

BRIEF SUMMARY OF THE INVENTION

In the present invention, which is an improvement to the directreduction process taught in U.S. Pat. No. 3,748,120, the process fuel isdesulfurized in the reduction furnace in a novel and useful manner byreacting the sulfur in the process fuel with hot direct reduced ironbefore the process fuel is admitted to the reformer. In effect, thesulfur in the process fuel is transferred to the iron during thereduction process, permitting sulfur levels as high as 400 ppmv in theprocess fuel to be tolerated without adding an undesirable amount ofsulfur to the direct reduced iron product. This in-situ desulfurizationof the process fuel makes practical, in the direct reduction of iron,the use of process fuels which are very difficult to desulfurizeexternally, such as coke oven gas or natural gas which contains organicsulfur compounds.

British Patent Specification No. 1,522,929 teaches a shaft furnace inwhich reducing gas is introduced at two vertically separated levels ofintroduction, one of which is around the periphery of the furnace, theother of which, being lower, is central of the furnace. In the presentapplication we introduce reducing gas at two vertically separatedlevels, but the reducing gas at each level has a different composition.In addition, both gases are introduced at different temperatures andboth are introduced around the periphery of the shaft furnace.

OBJECTS OF THE INVENTION

It is the primary object of this invention to provide means fordesulfurization of gaseous process fuel used for direct reduction ofiron by reacting sulfur present in the fuel with hot partially reducediron during the reduction process.

It is another object of the invention to provide a highly efficientprocess for the direct reduction of iron utilizing reforming ofhydrocarbon-containing gaseous process fuel to produce reducing gas, inwhich the process fuel is desulfurized in the reduction process prior tobeing reformed.

It is also an object of the invention to provide a direct reductionprocess which is particularly well adapted for the use of gaseousprocess fuels which contain organic sulfur.

It is a further object of the invention to provide apparatus forcarrying out the process.

BRIEF DESCRIPTION OF THE DRAWING

The single FIGURE is a diagrammatic illustration of the preferredembodiment of the invention.

DETAILED DESCRIPTION

Referring now to the drawing, a refractory-lined counterflow shaft typereduction furnace is indicated generally at 10. Iron oxide feed material12, in the form of oxide pellets, natural lump ore, or a mixture ofpellets and lump ore having a nominal particle size in the range of 5 to30 mm, is introduced to a feed hopper 14 and into the furnace through afeed pipe 16 to establish a burden 17 within the furnace. Particulatedirect reduced iron product is withdrawn from the lower region of thefurnace through a furnace discharge pipe 18 by a discharge conveyor 20,the speed of which controls the rate of descent of the burden 17 throughfurnace 10.

The middle region of furnace 10 is provided with a hot reducing gasinlet pipe 22 leading to a plurality of gas inlet ports 24 arranged inthe furnace refractory wall. A hot pre-reducing gas inlet pipe 26 isprovided leading to a plurality of gas inlet ports 28 arranged in thefurnace refractory wall at an elevation above ports 24. Hot pre-reducinggas, which consists of a mixture of hot reformed reducing gas and hotprocess fuel gas, introduced through ports 28 flows inwardly, thenupwardly in counterflow relationship to the descending burden. Hotreducing gas introduced through ports 24 also flows inwardly, thenupwardly in counterflow relationship to the descending burden. The hotreducing gas from ports 24, in its upward flow, initially fills theentire cross-section of the burden and then is forced to converge towardthe center region of the burden at about the elevation of ports 28 dueto the flow of hot pre-reducing gas through ports 28. In the upperregion of the furnace the two gas streams merge and fill the entirecross-section of the burden and exit the burden at stockline 30 andleave the furnace through top gas outlet pipe 32. The top gas whichleaves the furnace through outlet pipe 32 is a mixture of spent reducinggas and process fuel gas.

The lower region of furnace 10 is provided with a cooling gas circuitfor cooling the direct reduced iron prior to discharge. This coolingcircuit includes a cooling gas inlet 34 leading to a cooling gasdistributing member 36 within furnace 10, a cooling gas collectingmember 38 positioned above the distributing member within the furnace, acooling gas outlet 40, and an external gas recirculating system having acooler-scrubber 42 and a recirculating blower 44.

Top gas leaving furnace 10 through outlet pipe 32 is cooled and scrubbedof dust in a cooler-scrubber 46 and withdrawn into pipe 48. The majorportion of the cooled top gas in pipe 48 is compressed in a compressor50 and then admitted to a plurality of heat resisting alloy reformertubes 52, one of which is shown in the drawing. Each reformer tube 52 isfilled with refractory lump at the tube entry region and the remainingmajor portion is filled with nickel or cobalt reforming catalystindicated generally as 54. The reformer tubes are enclosed in arefractory lined reformer furnace 56 having a plurality of burners 58,one of which is shown, and a flue pipe 60 for venting the spent burnercombustion gases from the reformer furnace. A minor portion of cooledtop gas in pipe 48 together with fuel from an external source 62 isadmitted to each burner through pipe 64. The spent burner combustiongases in flue pipe 60 are utilized in a heat exchanger, not shown, topreheat combustion air for each burner from a source 66.

A process fuel gas heater 70, equipped with a plurality of heatresisting alloy heater tubes 72, one of which is shown, is provided forheating process fuel gas from a source 74. Heat is supplied to theheater by a plurality of burners 76, one of which is shown to whichburner fuel is admitted from a source 77 and combustion air from asource 78. Spent burner combustion gases leave the heater through a fluepipe 80. Heated process fuel gas is admitted to reduction furnace 10 viapipes 82 and 84 and pre-reducing gas inlet 26.

The first, usually the major, portion of the hot gas leaving reformertubes 52 is delivered to the hot reducing gas inlet 22, as the hotreformed reducing gas, via pipes 90 and 92. A second, usually minor,portion of the hot gas leaving reformer tubes 52 passes through pipe 94and valve 96, then is mixed with heated process fuel gas in pipe 84 andthis mixture becomes the hot prereducing gas admitted to furnace 10 atinlet 26.

The temperature of the process gas must be at least about 600° C., butis preferred to be above 650° C. The process gas must be heated to asufficiently high temperature that a mixture of process gas and heatedremoved top gas will have a sufficiently high temperature to carry outthe direct reduction of iron oxide.

In its broadest concept the invented process includes the completemixing of the sulfur-containing process gas, such as coke oven gas,natural gas or blast furnace gas, with the hot reformed reducing gas toform a reducing gas mixture. This mixture is then introduced to thereducing zone of the furnace through a single bustle and tuyere system.This process can be performed with the apparatus shown in the drawingmerely by the closing of valve 100 in pipe 84.

In the art of desulfurization of fuel gases such as natural gas, blastfurnace gas or coke oven gas, there are numerous well establishedcommercial processes for removing H₂ S (hydrogen sulfide) from suchgases in a single desulfurization step. However, the removal of COS(carbonyl sulfide) and organic sulfur compounds such as thiophene (C₄ H₄S) require the use of complicated and expensive multi-stagedesulfurization processes to hydrogenate and convert the sulfurcompounds to H₂ S before these forms of sulfur can be removed.

By laboratory experimentation, we have discovered that COS and organicsulfur compounds can be removed from gases by reaction with hot directreduced iron pellets in the presence of hydrogen. The direct reducediron is not effective at low temperatures for removal of these sulfurcompounds, but is effective at temperatures of about 700° C. and higher.The exact mechanism of this sulfur removal is not known to us, but webelieve the hot direct reduced iron becomes an effective catalyst forconversion of these sulfur compounds in the presence of hydrogen, to H₂S, which then chemically reacts with the iron. In any event, the sulfuris transferred from the gas to the direct reduced iron.

Therefore the gas mixture introduced to inlet 26 must be above about700° C. for sulfur removal. Higher temperatures are usually preferred,however, as at least about 800° C. is needed for direct reduction of theiron oxide. Some pellets cluster at 800° C., so they must be reduced atlower temperatures. A practical lower limit for the temperature of thegas to inlet 22 is thus 750° C.

The following is a specific example of the present invention, utilizingsulfur-containing coke oven gas as the process fuel gas, and for theburner fuel for both the reformer furnace and the process fuel gasheater. The sulfur level selected for the coke oven gas in this exampleis 200 ppmv which is a sulfur level commonly achieved by simple singlestep desulfurization processes. Gas with this level of sulfur, althoughunuseable as a process fuel for reforming, is very acceptable as aburner fuel.

In the specific example of this invention, and referring to the drawing,hot reducing gas from the reformer tubes 52 is admitted to the reductionfurnace at inlet 22 at a temperature of about 900° C. Hot pre-reducinggas, which is a mixture of 900° C. gas from the reformer tubes and 750°C. coke oven gas from heater tubes 72, is admitted to the reductionfurnace at inlet 26 at a temperature of about 800° C. The reductionfurnace design provides for a furnace burden residence time of about 4hours from the stockline 30 to ports 28 and 6 hours from stockline 30 toports 24, which insures that a high degree of direct reduction of theiron oxide to metallic iron is achieved in the pre-reduction zone aboveports 28, with the final degree of direct reduction being achieved inthe reduction zone between ports 24 and ports 28.

In the pre-reduction zone, the reductants CO and H₂ in the hotpre-reducing gas and in the hot reducing gas flowing up from the finalreduction zone reduce the iron oxide feed material to a degree ofmetallization of about 94 percent. Based upon both laboratory tests andcommercial experience, the methane present in the pre-reduction gas fromthe coke oven gas does not crack to any significant degree in itspassage through the pre-reduction zone at 800° C. because hydrogen isalready present in the gas. Thus, the spent reducing gas or top gasexiting from the furnace burden at the stockline and from the furnacegas outlet pipe 32 contains unreacted reductants CO and H₂, oxidants CO₂and H₂ O vapor formed in the reduction process, and methane. In the topgas cooler-scrubber 46, a major portion of the H₂ O vapor is condensedout of the top gas, resulting in a gas mixture suitable for reforming inreformer tubes 52 to produce hot fresh reducing gas. In the reformertubes, the CO₂ and residual water vapor in the cooled and scrubbed topgas serve as the reforming oxidants for the methane, as is set forth inU.S. Pat. No. 3,748,120.

The following tables show the results of a comprehensive processanalysis of the invented process and are keyed to the drawing. Thesedata are to be understood as being merely illustrative and in no waylimiting. All of the tabulations are based on one metric ton of directreduced iron product, having a degree of metallization of 92 percent anda carbon content of 1.5 percent. These are widely accepted commercialstandards for direct reduced iron produced in natural gas based directreduction plants.

Table I shows the fuel input required for the process. Coke oven gas hasa higher heating value of 4618 kCal/Nm³.

                  TABLE I                                                         ______________________________________                                                             Fuel Input                                               ______________________________________                                        Process Gas            2.82 Gcal                                              Reformer Burners       0.07                                                   Heater Burners         0.32                                                     Total Fuel Requirement                                                                             3.21 Gcal                                              ______________________________________                                    

Table II shows the gas flows in the process in normal cubic meters perhour at the indicated locations on the drawing.

                  TABLE II                                                        ______________________________________                                        Gas               Location   Flow Rate                                        ______________________________________                                        From Reformer     90         1320                                             To Lower Inlets   92          922                                             Reformed Gas to Upper Inlets                                                                    94          398                                             Heated Process Gas                                                                              82          609                                             Gas Mixture To Upper Inlets                                                                     84         1007                                             Reacted Top Gas   32         1901                                             Recycle Gas       48         1525                                             Gas Feed To Reformer                                                                            52         1085                                             Recycle Gas to Reformer Burner                                                                  64          440                                             ______________________________________                                    

Table III shows the gas analyses in percent at the locations indicated.

                                      TABLE III                                   __________________________________________________________________________    Gas        Location                                                                           CO CO.sub.2                                                                         H.sub.2                                                                          H.sub.2 O                                                                        CH.sub.4                                                                         N.sub.2                                                                         Sulfur (ppm)                                 __________________________________________________________________________    Reformed Gas                                                                             90   32.9                                                                             2.5                                                                              51.5                                                                             5.1                                                                              1.9                                                                              6.2                                            Process Fuel                                                                             82   6.8                                                                              1.8                                                                              54.3                                                                             3.0                                                                              28.7                                                                             5.4                                                                             200                                          To Upper Inlets                                                                          84   17.1                                                                             2.1                                                                              53.2                                                                             3.8                                                                              18.1                                                                             5.7                                                                             121                                          Top Gas    32   13.4                                                                             12.4                                                                             34.3                                                                             23.4                                                                             10.5                                                                             6.0                                            Cleaned Recycle Gas                                                                      48   16.7                                                                             15.5                                                                             42.7                                                                             4.5                                                                              13.1                                                                             7.5                                            __________________________________________________________________________

Approximately 0.018 percent sulfur is added to the metallized ironproduct by the sulfur transfer from the process fuel gas. This is belowthe acceptable limit of 0.03 percent for use of direct reduced iron inelectric arc furnace steelmaking.

In the present invention, when natural gas rather than coke oven gas isutilized as the process fuel gas, the required volumetric quantity ofthe natural gas will be approximately one-half that of coke oven gas dueto the almost twice calorific value of the natural gas. This will enablethe natural gas to contain approximately 400 ppmv of sulfur withoutadding an excessive amount of sulfur to the iron product.

Process fuel gases such as coke oven gas and naphtha vapor containunsaturated hydrocarbons which can present carbon deposition problems incatalytic reforming. The present process, in addition to desulfurizingthe process fuel gas, also serves to convert such unsaturatedhydrocarbons into methane or other saturated hydrocarbon in thereduction furnace prior to the reforming and thus avoids carbondeposition problems during reforming.

It can readily be seen from the foregoing, that we have invented animproved process for the direct reduction of iron which will allow thedirect use of sulfur-containing process fuel gases.

What is claimed is:
 1. Apparatus for direct reduction of iron oxides toa metallized iron product, said apparatus comprising:(a) a generallyvertical shaft furnace; (b) means for charging particulate iron oxidematerial to the upper portion of said furnace to form a burden therein,and means for removing metallized iron product from the bottom of saidfurnace, whereby a continuous gravitational flow of said burden can beestablished through the furnace; (c) a first hot reducing gas inletintermediate the ends of the furnace; (d) a second hot reducing gasinlet intermediate said first reducing gas inlet and the upper end ofthe furnace; (e) a reacted gas outlet at the upper end of said furnace;(f) means communicating with said reacted gas outlet for cooling andscrubbing reacted gas; (g) a reformer furnace with catalyst-containingtubes therein, for the formation of gaseous reductants, an inlet to saidreformer communicating with said cooling and scrubbing means, an outletfrom said reformer, a first conduit communicating with said reformeroutlet and said first reducing gas inlet, and a second conduitcommunicating with said reformer outlet and said second hot reducing gasinlet; (h) a process gas heater; (i) a source of process gascommunicating with said heater; and (j) a third conduit communicatingwith said heater and said second reducing gas inlet.
 2. Apparatusaccording to claim 1 further comprising means intermediate said firsthot reducing gas inlet and the bottom of said furnace for cooling themetallized iron product.
 3. Apparatus according to claim 1 furthercomprising valve means in said second conduit for controlling the flowof hot reducing gas from said reformer to said second hot reducing gasinlet.
 4. Apparatus according to claim 1 further comprising valve meansin said third conduit for controlling the flow of hot reducing gas tosaid second reducing gas inlet.